CN104671576A - Waste salt refining device and process in chemical industry - Google Patents
Waste salt refining device and process in chemical industry Download PDFInfo
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- CN104671576A CN104671576A CN201510077706.2A CN201510077706A CN104671576A CN 104671576 A CN104671576 A CN 104671576A CN 201510077706 A CN201510077706 A CN 201510077706A CN 104671576 A CN104671576 A CN 104671576A
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- 150000003839 salts Chemical class 0.000 title claims abstract description 81
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000007670 refining Methods 0.000 title claims abstract description 19
- 239000002699 waste material Substances 0.000 title abstract 3
- 239000000126 substance Substances 0.000 title abstract 2
- 238000001704 evaporation Methods 0.000 claims abstract description 17
- 238000001816 cooling Methods 0.000 claims abstract description 15
- 235000002639 sodium chloride Nutrition 0.000 claims description 88
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 48
- 239000007787 solid Substances 0.000 claims description 28
- 238000001354 calcination Methods 0.000 claims description 26
- 239000006200 vaporizer Substances 0.000 claims description 26
- 239000002351 wastewater Substances 0.000 claims description 22
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 19
- 238000002425 crystallisation Methods 0.000 claims description 16
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 238000003889 chemical engineering Methods 0.000 claims description 14
- 230000008025 crystallization Effects 0.000 claims description 13
- 238000010521 absorption reaction Methods 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 12
- 230000005494 condensation Effects 0.000 claims description 12
- 239000002562 thickening agent Substances 0.000 claims description 12
- 238000011084 recovery Methods 0.000 claims description 11
- 239000011347 resin Substances 0.000 claims description 10
- 229920005989 resin Polymers 0.000 claims description 10
- 239000011780 sodium chloride Substances 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 9
- 239000012047 saturated solution Substances 0.000 claims description 9
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical class O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 9
- 230000008020 evaporation Effects 0.000 claims description 7
- 239000012267 brine Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 5
- 238000002203 pretreatment Methods 0.000 claims description 5
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 239000000706 filtrate Substances 0.000 claims description 3
- 238000003837 high-temperature calcination Methods 0.000 claims description 3
- 230000003647 oxidation Effects 0.000 claims description 3
- 238000007254 oxidation reaction Methods 0.000 claims description 3
- 238000001953 recrystallisation Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- CZGCEKJOLUNIFY-UHFFFAOYSA-N 4-Chloronitrobenzene Chemical compound [O-][N+](=O)C1=CC=C(Cl)C=C1 CZGCEKJOLUNIFY-UHFFFAOYSA-N 0.000 description 10
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 10
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 10
- 239000007789 gas Substances 0.000 description 10
- 239000012452 mother liquor Substances 0.000 description 8
- 238000001179 sorption measurement Methods 0.000 description 8
- 150000002500 ions Chemical class 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 6
- CURNJKLCYZZBNJ-UHFFFAOYSA-M sodium;4-nitrophenolate Chemical compound [Na+].[O-]C1=CC=C([N+]([O-])=O)C=C1 CURNJKLCYZZBNJ-UHFFFAOYSA-M 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000004806 packaging method and process Methods 0.000 description 5
- 239000003444 phase transfer catalyst Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 239000007795 chemical reaction product Substances 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 238000006460 hydrolysis reaction Methods 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 3
- 239000003610 charcoal Substances 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000008236 heating water Substances 0.000 description 3
- BFCFYVKQTRLZHA-UHFFFAOYSA-N 1-chloro-2-nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1Cl BFCFYVKQTRLZHA-UHFFFAOYSA-N 0.000 description 2
- BTJIUGUIPKRLHP-UHFFFAOYSA-N 4-nitrophenol Chemical compound OC1=CC=C([N+]([O-])=O)C=C1 BTJIUGUIPKRLHP-UHFFFAOYSA-N 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000012266 salt solution Substances 0.000 description 2
- 230000035943 smell Effects 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 239000002932 luster Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 239000010891 toxic waste Substances 0.000 description 1
Landscapes
- Water Treatment By Sorption (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a waste salt refining device and a waste salt refining process in the chemical industry. The device is characterized by comprising an adsorber, evaporating crystallizers, a centrifugal machine, a rotary kiln, a dissolver, a filter, an incinerator, a cooling tower and an exhaust tower, wherein the adsorber is connected with the centrifugal machine by virtue of a first evaporating crystallizer; the discharge opening of the centrifugal machine is connected with the rotary kiln; the discharge opening of the rotary kiln is connected with a dissolving tank; the dissolving tank is connected with a second evaporating crystallizer by virtue of the filter; the second evaporating crystallizer is connected with the centrifugal machine; the air outlet of the rotary kiln is connected with the incinerator; and the incinerator is connected with the exhaust tower by virtue of the cooling tower.
Description
Technical field
The invention belongs to abraum salt process for refining, is a kind of chemical engineering industry abraum salt refining plant and technique specifically.
Background technology
Utilizing para-nitrochloro-benzene, ortho-nitrochlorobenzene produces amino phenylate; Produce with para-nitrochloro-benzene in the process of p-NP, a large amount of sodium-chlor can be generated, produce a large amount of high salt, high COD, highly toxic waste water.High-salt wastewater must take effective treatment measures to process.Otherwise, serious environmental pollution will be caused.When the salts contg in waste water reaches 2%, during biochemical treatment, bacterium is difficult to survival, and time biochemical, the salts contg in general waste water controls below 1.5%, and the method for control is thin up.Along with environmental requirement is more and more higher, at present, do not allow thin up, the method for evaporation must be adopted, salt from being steamed out waste water.The salt be evaporated, due to containing a certain amount of organism, and with some smells, can not use as industrial salt.Can not sell as by-product, some enterprise is deposited in on-site solid salt, some illegal retailer, this other additives of salt blending is made Snow Agent and sells, certainly will bring new pollution.If as solid waste, the fixed-end forces company must giving qualification processes.Give the process of professional solid waste company, the handling that more than 4000 yuan will be received per ton.
High-concentration salt-containing wastewater, the method for useful liquid waste incinerator directly burns to process, and energy consumption is high, and burn not thorough, salt slag is impure many, can not recycle.Can only stack, will certainly secondary pollution be produced.
Abraum salt thermal degradation, to re-refine be the feasible solution of a kind of harmless treatment, resource reutilization.A kind of method and equipment (patent No.: ZL200510031311.5) thereof recycling industrial waste salt, describe a kind of multi-layer discs process furnace, the high-temperature flue gas of 350-1000 DEG C is passed in stove, the warm air of 300-800 DEG C is led in stove, at such high temperatures, enough physical strengths can also be ensured, in heat-processed without any metal, objectionable impurities can not be decomposed completely, also has to pass through the service requirements of refining ability chlor-alkali industry.
Summary of the invention
For above-mentioned deficiency, the invention provides a kind of recovery utilization rate high, pollution-free, the chemical engineering industry abraum salt refining plant of environmental protection and economy and technique.
The technical solution used in the present invention is: a kind of chemical engineering industry abraum salt refining plant, comprise adsorber, evaporative crystallizer, whizzer, rotary kiln, dissolver, strainer, incinerator, cooling tower and discharge tower, adsorber connects whizzer through the first evaporative crystallizer, whizzer discharging connects rotary kiln, rotary kiln discharging connects dissolving vessel, dissolving vessel connects the second evaporative crystallizer through filter, second evaporative crystallizer connects whizzer, rotary kiln is given vent to anger connection incinerator, and incinerator connects discharge tower through cooling tower.
Further, described evaporative crystallizer comprises preheater, condensation water pot, vaporizer, crystallizer and vapour compressor, preheater one end connects adsorber, preheater the other end feed connects bottom the evaporator room of vaporizer, the evaporator room top of vaporizer connects the evaporator room top of crystallizer, the evaporator room top of crystallizer connects the heating chamber top of vaporizer through vapour compressor, the heating chamber bottom of vaporizer is successively through condensation water pot, pump connects preheater, the separate chamber of crystallizer bottom connects bottom the evaporator room of vaporizer, the crystallizing bed of crystalliser feet connects whizzer through pump.
Further, tundish, pump, adjustment still and pump is provided with between described adsorber and the first evaporative crystallizer successively.
Further, the crystallizing bed of described crystalliser feet connects thickener through pump, and thickener connects whizzer.
Chemical engineering industry abraum salt process for refining: the high-salt wastewater pre-treatment that contains in amino phenylate, p-NP production process is regulated pH value, adsorbed by gac or diatomite or macroporous resin, remove the organism in waste water and organic salt, reduce the COD of waste water, then high-salt wastewater is adjusted to neutrality, carry out evaporating through multiple-effect evaporation or mechanical recompression, crystallization, centrifugal go out solid salt; By centrifugal go out solid salt through rotary kiln or tunnel furnace high-temperature calcination, organism is made at high temperature to decompose oxidation, the tail gas of calcining thoroughly burns through heat accumulating type tail gas burning furnace again, tail gas is through pre-recovery of heat, spray-absorption, salt after calcining is made into saturated solution with after water-solubleization, filter through accurate filter, filtrate directly supplies ion film caustic soda and uses, maybe the saturated brine after filtering is carried out evaporating through multiple-effect evaporation or mechanical recompression, recrystallization purifies, by centrifugal, obtain the solid sodium chloride of high-quality.
Further, effluent brine pre-treatment: can uncomfortable pH value with the diatomite used time, when adsorbing with gac or macroporous resin, pH value modulation 1-5.
Further, in calcination process, the residence time of material is 2-4 hour, and calcining temperature is 300-800 DEG C, is no more than the fusing point of salt.
Again further, incinerator is fixed bed or rotating bed, and tail gas incineration temperature is 800-1000 DEG C.
When producing amino phenylate, p-NP, containing the first pre-treatment of high-salt wastewater, pretreatment process is: high-salt wastewater is regulated pH value, high-salt wastewater is adsorbed by gac, diatomite or macroporous resin, remove the organism in waste water and organic salt, reduce the COD of waste water, then high-salt wastewater carry out evaporating through multiple-effect evaporation or mechanical recompression (MVR), crystallization, by centrifugal, isolate solid salt.Solid salt now, still containing a certain amount of organism, also has certain smell, the color and luster of salt, in white or micro-Huang, containing a certain amount of ammonia nitrogen, also thoroughly must remove the organism in salt, by the way of absorption, extraction, the object removing micro-content organism can not be reached.The present invention is by this salt through rotary kiln or tunnel furnace high-temperature calcination, and calcining temperature is 300-800 DEG C, makes organism at high temperature, decompose oxidation, the tail gas of calcining thoroughly burns through heat accumulating type tail gas burning furnace again, and tail gas is through pre-recovery of heat, spray-absorption, reaches harmless discharge.Salt after calcining reaches the service requirements of ion film caustic soda, soda industry completely, by salt with after water-solubleization, is made into saturated solution, filters through accurate filter, and filtrate can be sold to ion film caustic soda enterprise and use.Also can saturated brine carry out evaporating through multiple-effect evaporation or mechanical recompression (MVR), recrystallization purifies, by centrifugal, obtain the solid sodium chloride of high-quality.Achieve the resource utilization regeneration of abraum salt, existing environmental benefit has economic worth again.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
In figure: adsorption tower 1, tundish 2, first pump 3, regulate still 4, second pump 5, first preheater 6, 3rd pump 7, first condensation water pot 8, first vaporizer 9, first vapour compressor 10, first crystallizer 11, 4th pump 12, first thickener 13, first whizzer 14, rotary kiln 15, burner 16, incinerator 17, cooling tower 18, vent gas tower 19, dissolving vessel 20, 5th pump 21, strainer 22, storage tank 23, second preheater 24, 6th pump 25, second condensation water pot 26, second vaporizer 27, second vapour compressor 28, second crystallizer 29, 7th pump 30, second thickener 31, second whizzer 32, 8th pump 33.
Embodiment
Below in conjunction with drawings and Examples, the invention will be further described.
Shown in Fig. 1, a kind of chemical engineering industry abraum salt refining plant comprises adsorption tower 1, tundish 2, first pump 3, regulate still 4, second pump 5, first preheater 6, 3rd pump 7, first condensation water pot 8, first vaporizer 9, first vapour compressor 10, first crystallizer 11, 4th pump 12, first thickener 13, first whizzer 14, rotary kiln 15, burner 16, incinerator 17, cooling tower 18, vent gas tower 19, dissolving vessel 20, 5th pump 21, strainer 22, storage tank 23, second preheater 24, 6th pump 25, second condensation water pot 26, second vaporizer 27, second vapour compressor 28, second crystallizer 29, 7th pump 30, second thickener 31, second whizzer 32 and the 8th pump 33.Adsorption tower 1 top charging, bottom connects tundish 2, tundish 2 connect adjustment still 4 through the first pump 3, still 4 is regulated to connect the first preheater 6 through the second pump 5, first preheater 6 connects bottom the evaporator room of the first vaporizer 9, the evaporator room top of the first vaporizer 9 connects the top of the first crystallizer 11, top first vapour compressor 10 of the first crystallizer 11 connects the heating chamber top of the first vaporizer 9, the heating chamber bottom of the first vaporizer 8 connects the first condensation water pot 8, first condensation water pot 8 connects the first preheater 6 through the 3rd pump 7, the separate chamber of the first crystallizer 11 bottom connects bottom the evaporator room of the first vaporizer 9, crystallizing bed bottom first crystallizer 11 connects the first thickener 13 through the 4th pump 12, first thickener 13 connects the first whizzer 14, first whizzer 14 discharging connects rotary kiln 15, rotary kiln 15 is given vent to anger the incinerator 17 of connecting band burner 16, incinerator 17 connects cooling tower 18, cooling tower 18 connects vent gas tower 19, rotary kiln 15 discharging connects dissolving vessel 20, dissolving vessel 20 connects strainer 22 through the 5th pump 21, strainer 22 connects storage tank 23, storage tank 23 connects the second preheater 24 through the 6th pump 25, second preheater 6 connects bottom the evaporator room of the second vaporizer 27, the evaporator room top of the second vaporizer 27 connects the top of the second crystallizer 29, top second vapour compressor 28 of the second crystallizer 29 connects the heating chamber top of the second vaporizer 27, the heating chamber bottom of the second vaporizer 27 connects the second condensation water pot 26, second condensation water pot 26 connects the second preheater 24 through the 8th pump 33, the separate chamber of the second crystallizer 29 bottom connects bottom the evaporator room of the second vaporizer 27, crystallizing bed bottom second crystallizer 29 connects the second thickener 31 through the 7th pump 30, second thickener 31 connects the second whizzer 32.
The technique of this device is:
Embodiment one:
Ethanol, para-nitrochloro-benzene, phase-transfer catalyst are joined in reactor, drips the NaOH solution of 50-75%, react at 60-65 DEG C.After reaction terminates, heating water dilutes, and makes the salt of lower floor soluble in water, and reaches the saturation concentration of sodium-chlor, then leave standstill, layering.Remove the reaction product on upper strata, the effluent brine of lower floor, add hydrochloric acid and regulate pH value, make PH=1-3, through charcoal absorption tar removing, azo, then go macroporous resin adsorption to remove p-NP, the salt solution NaOH after absorption is adjusted to neutrality.Through MVR evaporative crystallization, centrifugally obtain solid salt, then by solid salt through the temperature lower calcination 2-3 hour of rotary kiln at 400-750 DEG C, the salt after calcining is after cooling, and packaging is sold.In salt, sodium chloride content is 96.4%, and the rate of recovery reaches 98%.
Embodiment two:
Solid ortho-nitrochlorobenzene is melt into liquid, throw in reactor, add ethanol, phase-transfer catalyst, at 55-60 DEG C, drip the liquid NaOH of 75%, after reaction terminates, heating water washs, stratification, by saliferous mother liquor furnishing PH=7, through charcoal absorption tar removing, azo, mother liquor is through MVR evaporative crystallization, centrifugally obtain solid salt, then by solid salt through the temperature lower calcination 3-4 hour of rotary kiln at 400-750 DEG C, salt after calcining is made into saturated solution, filter through accurate filter, again through MVR evaporative crystallization, centrifugally obtain solid salt, after drying, packaging is sold.In salt, sodium chloride content is 95.5%, and the rate of recovery reaches 97%.
Embodiment three:
Ethanol, para-nitrochloro-benzene, phase-transfer catalyst are joined in reactor, drips the NaOH solution of 50-75%, react at 60-65 DEG C.After reaction terminates, heating water dilutes, and makes the salt of lower floor soluble in water, and reaches the saturation concentration of sodium-chlor, then leave standstill, layering.Remove the reaction product on upper strata, the effluent brine of lower floor, add hydrochloric acid and regulate pH value, make PH=1-3, through charcoal absorption tar removing, azo, then go macroporous resin adsorption to remove p-NP, the salt solution NaOH after absorption is adjusted to neutrality.Through MVR evaporative crystallization, centrifugally obtain solid salt, then by solid salt through the temperature lower calcination 2-3 hour of rotary kiln at 400-750 DEG C, salt after calcining is made into saturated solution, filter through accurate filter, then through MVR evaporative crystallization, centrifugally obtain solid salt, after drying packaging, for ion film caustic soda.In salt, sodium chloride content is 99.4%, and the rate of recovery reaches 96%.
Embodiment four:
Ethanol, para-nitrochloro-benzene, phase-transfer catalyst are joined in reactor, drips solid NaOH, react at 60-65 DEG C.After reaction terminates, leave standstill, layering.Remove the reaction product on upper strata, the effluent brine of lower floor goes centrifugal together with salt, the centrifugal solid salt obtained, and through the temperature lower calcination 3-4 hour of rotary kiln at 400-750 DEG C, the salt after calcining is made into saturated solution, filters, for soda factory through accurate filter.The rate of recovery reaches 99%.
Embodiment five:
Ethanol, para-nitrochloro-benzene, phase-transfer catalyst are joined in reactor, drips solid NaOH, react at 60-65 DEG C.After reaction terminates, leave standstill, layering.Remove the reaction product on upper strata, the effluent brine of lower floor goes centrifugal together with salt, the centrifugal solid salt obtained, through the temperature lower calcination 3-4 hour of rotary kiln at 400-750 DEG C, the salt after calcining is made into saturated solution, filters through accurate filter, again through MVR evaporative crystallization, centrifugally obtain solid salt, after drying, packaging is sold.Reach the service requirements of ion film caustic soda.In salt, sodium chloride content is 98.5%, and the rate of recovery reaches 97%.
Embodiment six:
Be that the sodium hydroxide solution of 10-15% adds in hydrolyzer by concentration, then add the p-Nitrophenyl chloride of melting, be heated to 150 DEG C, then stop heating, hydrolysis reaction heat release makes temperature and pressure naturally rise to 165 DEG C, 0.7MPa.P-Nitrophenyl chloride obtains Sodium p-nitrophenoxide through hydrolysis reaction, then crystallisation by cooling, the mother liquor after centrifugal mainly contains the high-salt wastewater of Sodium p-nitrophenoxide and sodium-chlor, adds hydrochloric acid and regulates pH value, make PH=1-4, Sodium p-nitrophenoxide acidifying is made to become p-nitrophenol, after activated carbon filtration, then through macroporous resin adsorption p-nitrophenol, mother liquor after absorption is evaporated by MVR, after crystallization is centrifugal, solid salt through calcining 2-3 hour, after cooling, pack sale.In salt, sodium chloride content is 98.5%, and the rate of recovery reaches 96%.
Embodiment seven:
P-Nitrophenyl chloride obtains Sodium p-nitrophenoxide through hydrolysis reaction, then crystallisation by cooling, mother liquor after centrifugal mainly contains the high-salt wastewater of Sodium p-nitrophenoxide and sodium-chlor, add hydrochloric acid and regulate pH value, make PH=1-4, Sodium p-nitrophenoxide acidifying is made to become p-NP, after activated carbon filtration, again through macroporous resin adsorption p-NP, the mother liquor after absorption is evaporated by MVR, after crystallization is centrifugal, solid salt through calcining 2-2.5 hour, salt after calcining is made into saturated solution, filters, for ion film caustic soda or soda industry through accurate filter.
Embodiment eight:
P-Nitrophenyl chloride obtains Sodium p-nitrophenoxide through hydrolysis reaction, then crystallisation by cooling, mother liquor after centrifugal mainly contains the high-salt wastewater of Sodium p-nitrophenoxide and sodium-chlor, add hydrochloric acid and regulate pH value, make PH=1-4, Sodium p-nitrophenoxide acidifying is made to become p-NP, after activated carbon filtration, again through macroporous resin adsorption p-NP, mother liquor after absorption is evaporated by MVR, after crystallization is centrifugal, solid salt through calcining 2.5-3.5 hour, salt after calcining is made into saturated solution, filter through accurate filter, remove undecomposed impurity and carbide, saturated aqueous common salt after filtration also can again through MVR evaporative crystallization, centrifugally obtain solid salt, after drying, packaging is sold.Reach the service requirements of ion film caustic soda completely.In salt, sodium chloride content is 99.5%, and the rate of recovery reaches 96%.
Claims (8)
1. a chemical engineering industry abraum salt refining plant, it is characterized in that: comprise adsorber, evaporative crystallizer, whizzer, rotary kiln, dissolver, strainer, incinerator, cooling tower and discharge tower, adsorber connects whizzer through the first evaporative crystallizer, whizzer discharging connects rotary kiln, rotary kiln discharging connects dissolving vessel, and dissolving vessel connects the second evaporative crystallizer through filter, and the second evaporative crystallizer connects whizzer, rotary kiln is given vent to anger connection incinerator, and incinerator connects discharge tower through cooling tower.
2. a kind of chemical engineering industry abraum salt refining plant according to claim 1, it is characterized in that: described evaporative crystallizer comprises preheater, condensation water pot, vaporizer, crystallizer and vapour compressor, preheater one end connects adsorber, preheater the other end feed connects bottom the evaporator room of vaporizer, the evaporator room top of vaporizer connects the evaporator room top of crystallizer, the evaporator room top of crystallizer connects the heating chamber top of vaporizer through vapour compressor, the heating chamber bottom of vaporizer is successively through condensation water pot, pump connects preheater, the separate chamber of crystallizer bottom connects bottom the evaporator room of vaporizer, the crystallizing bed of crystalliser feet connects whizzer through pump.
3. a kind of chemical engineering industry abraum salt refining plant according to claim 1, is characterized in that: be provided with tundish, pump, adjustment still and pump between described adsorber and the first evaporative crystallizer successively.
4. a kind of chemical engineering industry abraum salt refining plant according to claim 1, is characterized in that: the crystallizing bed of described crystalliser feet connects thickener through pump, and thickener connects whizzer.
5. a chemical engineering industry abraum salt process for refining, it is characterized in that: the high-salt wastewater pre-treatment that contains in amino phenylate, p-NP production process is regulated pH value, adsorbed by gac or diatomite or macroporous resin, remove the organism in waste water and organic salt, reduce the COD of waste water, then high-salt wastewater is adjusted to neutrality, carries out evaporating through multiple-effect evaporation or mechanical recompression, crystallization, centrifugal go out solid salt; By centrifugal go out solid salt through rotary kiln or tunnel furnace high-temperature calcination, organism is made at high temperature to decompose oxidation, the tail gas of calcining thoroughly burns through heat accumulating type tail gas burning furnace again, tail gas is through pre-recovery of heat, spray-absorption, salt after calcining is made into saturated solution with after water-solubleization, filter through accurate filter, filtrate directly supplies ion film caustic soda and uses, maybe the saturated brine after filtering is carried out evaporating through multiple-effect evaporation or mechanical recompression, recrystallization purifies, by centrifugal, obtain the solid sodium chloride of high-quality.
6. a kind of chemical engineering industry abraum salt process for refining according to claim 1, is characterized in that, effluent brine pre-treatment: can uncomfortable pH value with the diatomite used time, when adsorbing with gac or macroporous resin, and pH value modulation 1-5.
7. a kind of chemical engineering industry abraum salt process for refining according to claim 1 and equipment, is characterized in that, in calcination process, the residence time of material is 2-4 hour, and calcining temperature is 300-800 DEG C, is no more than the fusing point of salt.
8. a kind of chemical engineering industry abraum salt process for refining according to claim 1 and equipment, is characterized in that, incinerator is fixed bed or rotating bed, and tail gas incineration temperature is 800-1000 DEG C.
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| CN201510077706.2A CN104671576B (en) | 2015-02-13 | 2015-02-13 | Waste salt refining device and process in chemical industry |
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| CN201510077706.2A CN104671576B (en) | 2015-02-13 | 2015-02-13 | Waste salt refining device and process in chemical industry |
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| CN104671576B CN104671576B (en) | 2017-04-19 |
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN109665660A (en) * | 2017-10-16 | 2019-04-23 | 孙汝友 | The refining methd of industrial waste salt |
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| CN111362282A (en) * | 2020-04-22 | 2020-07-03 | 利民化学有限责任公司 | Production method and system for recycling sodium chloride from phenylguanidine carbonate synthetic wastewater |
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| CN105293531A (en) * | 2015-11-26 | 2016-02-03 | 山东潍坊润丰化工股份有限公司 | Byproduct industrial salt refined processing method |
| CN106007078A (en) * | 2016-07-05 | 2016-10-12 | 双良节能系统股份有限公司 | Intermittent adsorption-catalytic oxidation treatment method for removing organic matters of coal chemical high-salt water |
| CN106495384A (en) * | 2016-11-03 | 2017-03-15 | 南京格洛特环境工程股份有限公司 | The technique that a kind of utilization organic contamination high-salt wastewater prepares industrial purified salt |
| CN106495384B (en) * | 2016-11-03 | 2020-04-07 | 南京格洛特环境工程股份有限公司 | Process for preparing industrial refined salt by utilizing organic pollution high-salinity wastewater |
| WO2018082343A1 (en) * | 2016-11-03 | 2018-05-11 | 南京格洛特环境工程股份有限公司 | Process for using organic high-salt wastewater to prepare industrial refined salt |
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| CN109665660A (en) * | 2017-10-16 | 2019-04-23 | 孙汝友 | The refining methd of industrial waste salt |
| CN107673531B (en) * | 2017-10-24 | 2020-06-16 | 北京今大禹环境技术股份有限公司 | High-salt high-organic-matter wastewater thermal membrane coupling salt separation zero-discharge treatment process |
| CN107673531A (en) * | 2017-10-24 | 2018-02-09 | 北京今大禹环境技术股份有限公司 | A kind of high organic wastewater hotting mask coupling of high salt divides salt Zero-discharge treating process |
| CN107651799A (en) * | 2017-10-24 | 2018-02-02 | 北京今大禹环境技术股份有限公司 | A kind of high organic wastewater hotting mask coupling of high salt divides salt zero-discharge treatment system |
| CN107651801A (en) * | 2017-10-24 | 2018-02-02 | 北京今大禹环境技术股份有限公司 | A kind of high organic wastewater hotting mask coupling Zero-discharge treating process of high salt |
| CN107651801B (en) * | 2017-10-24 | 2020-06-16 | 北京今大禹环境技术股份有限公司 | High-salt high-organic-matter wastewater thermal membrane coupling zero-emission treatment process |
| CN107651799B (en) * | 2017-10-24 | 2020-06-16 | 北京今大禹环境技术股份有限公司 | High-salinity high-organic-matter wastewater thermal membrane coupling salt separation zero-discharge treatment system |
| CN109019634A (en) * | 2018-07-18 | 2018-12-18 | 南京简迪环境工程有限公司 | The purification of chemical industry abraum salt and resource utilization system and method |
| CN109019634B (en) * | 2018-07-18 | 2021-03-26 | 南京简迪环境工程有限公司 | Chemical waste salt refining and resource utilization system and method |
| CN109078582A (en) * | 2018-07-31 | 2018-12-25 | 南京格洛特环境工程股份有限公司 | Distillation and reaction residue treatment process |
| CN110397940A (en) * | 2019-07-23 | 2019-11-01 | 源创环境科技有限公司 | A kind of technique of high temperature incineration processing landfill leachate |
| CN111362282A (en) * | 2020-04-22 | 2020-07-03 | 利民化学有限责任公司 | Production method and system for recycling sodium chloride from phenylguanidine carbonate synthetic wastewater |
| CN114249336A (en) * | 2021-12-30 | 2022-03-29 | 盐城市国投环境技术股份有限公司 | Process for preparing industrial sodium carbonate by using chemical tail gas waste salt |
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